CATALYST BASED ON y-KETOVALERIC ACID AND USE THEREOF IN A HYDROTREATMENT AND/OR HYDROCRACKING PROCESS

ABSTRACT

The invention relates to a catalyst comprising a support based on alumina or silica or silica-alumina, at least one element of group VIII, at least one element of group VIB and γ-ketovaleric acid. The invention also relates to the process for the preparation of said catalyst and the use thereof in a hydrotreatment and/or hydrocracking process.

The invention relates to a catalyst with the additive γ-ketovalericacid, the method for the preparation thereof and the use thereof in thefield of hydrotreatment and/or hydrocracking.

A catalyst for the hydrotreatment of hydrocarbon-containing cuts usuallyhas the aim of removing the sulphur-containing or nitrogen-containingcompounds contained therein so that for example a petroleum productmeets the required specifications (sulphur content, aromatics contentetc.) for a given application (motor fuel, gasoline or gasoil, domesticfuel oil, jet fuel). It may also be a question of pre-treating thisfeedstock in order to remove impurities from it or to hydrogenate itbefore subjecting it to various conversion processes for modifying itsphysicochemical properties, such as for example processes of reforming,hydrocracking of vacuum distillates, catalytic cracking, hydroconversionof atmospheric or vacuum residues. The composition and the use ofhydrotreatment catalysts are described particularly well in the articleby B. S. Clausen, H. T. Topsøe, and F. E. Massoth, from the workCatalysis Science and Technology, volume 11 (1996), Springer-Verlag.

Stricter vehicle pollution standards in the European Community (OfficialJournal of the European Union, L76, 22 Mar. 2003, Directive 2003/70/CE,pages L76/10-L76/19) have compelled refiners to dramatically reduce thesulphur content of diesel fuels and gasolines (to a maximum of 10 partsper million by weight (ppm) of sulphur on 1 Jan. 2009, against 50 ppm on1 Jan. 2005). Moreover, the refiners are compelled to use feedstocksthat are more and more refractory to hydrotreatment processes on the onehand because the crude oils are becoming increasingly heavy andconsequently contain an increasing amount of impurities, and on theother hand owing to the increasing use of conversion processes inrefineries. In fact, these generate cuts that are more difficult tohydrotreat than the cuts originating directly from atmosphericdistillation. By “more difficult to hydrotreat” is usually meant higheroperating temperatures to achieve the same sulphur content in theeffluent, and consequently cycle times that can be reduced. Thesefeedstocks require catalysts having hydrodesulphurizing andhydrogenating functions that are greatly improved with respect toconventional catalysts.

Moreover, conversion processes such as catalytic cracking orhydrocracking use catalysts having an acid function, which makes themparticularly sensitive to the presence of nitrogen-containingimpurities, and especially basic nitrogen-containing compounds. It istherefore necessary to use catalysts for pre-treatment of thesefeedstocks so as to remove these compounds.

Conventional hydrotreatment catalysts generally comprise an oxidesupport and an active phase based on metals of groups VIB and VIII intheir oxide forms, as well as phosphorus. Preparation of these catalystsgenerally comprises a step of impregnation of the metals and of thephosphorus on the support, followed by drying and calcination making itpossible to obtain the active phase in their oxide forms. Before theyare used in a hydrotreatment and/or hydrocracking reaction, thesecatalysts are generally subjected to sulphurization in order to form theactive species.

The addition of an organic compound to hydrotreatment catalysts in orderto improve their activity has been recommended by a person skilled inthe art, in particular for catalysts that have been prepared byimpregnation followed by drying without subsequent calcination. Thesecatalysts are often called “additive-impregnated dried catalysts”.

Many documents describe the use of various ranges of organic compoundsas additives, such as nitrogen-containing organic compounds and/oroxygen-containing organic compounds.

A family of compounds that is now well known from the literature is thechelating nitrogen-containing compounds (EP0181035, EP1043069 and U.S.Pat. No. 6,540,908) with, by way of example, ethylenediaminetetraaceticacid (EDTA), ethylenediamine, diethylenetriamine or nitrilotriaceticacid (NTA).

In the family of organic compounds containing oxygen, the use of mono-,di- or polyols, optionally etherified, is described in documentsWO96/41848, WO01/76741, U.S. Pat. No. 4,012,340, U.S. Pat. No.3,954,673, EP601722, and WO2005/035691. More rarely, the prior artmentions additives comprising ester functions (EP1046424,WO2006/077326).

There are also several patents that claim the use of carboxylic acids(EP1402948, EP0482817). In particular, in document EP0482817, citricacid, but also tartaric, butyric, hydroxyhexanoic, malic, gluconic,glyceric, glycolic, hydroxybutyric acids have been described. Thespecificity is based on the drying, which must be carried out at atemperature of less than 200° C. However, none of the documents relatingto the carboxylic acids describes the use of γ-ketovaleric acid.

Whatever compounds are selected, the modifications induced do not alwaysmake it possible to increase catalyst performance sufficiently to meetthe specifications relating to the sulphur and/or nitrogen contents ofmotor fuels. Moreover, it is often very complicated to apply themindustrially, as the methods are complex to implement.

Consequently, it proves to be essential for catalyst manufacturers tofind new hydrotreatment and/or hydrocracking catalysts with improvedperformance.

SUMMARY

The invention relates to a catalyst comprising a support based onalumina or silica or silica-alumina, at least one element of group VIII,at least one element of group VIB and γ-ketovaleric acid.

The applicant in fact found that the use of γ-ketovaleric acid as anorganic additive on a catalyst containing at least one element of groupVIII and at least one element of group VIB allowed a hydrotreatmentand/or hydrocracking catalyst with improved catalytic performance to beobtained.

In fact, the catalyst according to the invention shows increasedactivity with respect to the catalysts without additives and to theknown dried catalysts with additives. Typically, owing to the increasein activity, the temperature required to reach a desired sulphur ornitrogen content (for example 10 ppm of sulphur in the case of a gasoilfeedstock, in ULSD or Ultra Low Sulphur Diesel mode) may be lowered.Moreover, stability is increased, as the cycle time is prolonged due tothe decrease in the required temperature.

The catalyst according to the present invention is moreover easy toprepare due to the high solubility of γ-ketovaleric acid in water or anyother polar protic solvent. Furthermore, the catalyst according to theinvention may be prepared from a raw material originating from biomasspreferably containing γ-ketovaleric acid while remaining at anacceptable or even advantageous cost price depending on the chosenpreparation process.

According to a variant, the content of the element of group VIB isbetween 5 and 40% by weight expressed as oxide of the metal of group VIBwith respect to the total weight of the catalyst, and the content of theelement of group VIII is comprised between 1 and 10% by weight expressedas oxide of the metal of group VIII with respect to the total weight ofthe catalyst.

According to a variant, the molar ratio of the element of group VIII tothe element of group VIB in the catalyst is comprised between 0.1 and0.8.

According to a variant, the catalyst additionally contains phosphorus,the phosphorus content being comprised between 0.1 and 20% by weightexpressed as P₂O₅ with respect to the total weight of the catalyst andthe ratio of phosphorus to the element of group VIB in the catalyst isgreater than or equal to 0.05.

According to a variant, the content of γ-ketovaleric acid is comprisedbetween 1 and 35% by weight with respect to the total weight of thecatalyst.

According to a variant, the catalyst additionally contains an organiccompound other than γ-ketovaleric acid containing oxygen and/or nitrogenand/or sulphur. According to this variant, the organic compound ispreferably selected from a compound comprising one or more chemicalfunctions selected from a carboxyl, alcohol, thiol, thioether, sulphone,sulphoxide, ether, aldehyde, ketone, ester, carbonate, amine, nitrile,imide, oxime, urea and amide function. Preferably, it is selected fromtriethylene glycol, diethylene glycol, ethylenediaminetetraacetic acid(EDTA), maleic acid, citric acid, dimethylformamide, bicine, or tricine.

According to a variant, the support contains from 0.1 to 50% by weightof zeolite.

According to a variant, the catalyst is at least partially sulphurized.

The invention also relates to the process for the preparation of saidcatalyst comprising the following steps:

-   -   a) bringing at least one component of an element of group VIB,        at least one component of an element of group VIII,        γ-ketovaleric acid and optionally phosphorus into contact with a        support based on alumina or silica or silica-alumina, or        bringing a regenerated catalyst containing a support based on        alumina or silica or silica-alumina, at least one component of        an element of group VIB, at least one component of an element of        group VIII and optionally phosphorus into contact with        γ-ketovaleric acid, so as to obtain a catalyst precursor,    -   b) drying said catalyst precursor originating from step a) at a        temperature of less than 200° C., without calcining it        subsequently.

According to a variant, step a) is the following step:

-   -   a′) impregnating a support based on alumina or silica or        silica-alumina with at least one solution containing at least        one element of group VIB, at least one element of group VIII,        γ-ketovaleric acid and optionally phosphorus so as to obtain a        catalyst precursor.

According to another variant, step a) comprises the following steps:

-   -   a1) impregnating a support based on alumina or silica or        silica-alumina with at least one solution containing at least        one element of group VIB, at least one element of group VIII and        optionally phosphorus in order to obtain an impregnated support,    -   a2) drying the impregnated support obtained in step a1) at a        temperature of less than 200° C. in order to obtain a dried        impregnated support, and optionally calcining the dried        impregnated support in order to obtain a calcined impregnated        support,    -   a3) impregnating the dried and optionally calcined impregnated        support obtained in step a2) with an impregnating solution        comprising at least γ-ketovaleric acid so as to obtain a        catalyst precursor,    -   a4) optionally, leaving the catalyst precursor obtained in step        a3) to mature.

According to another variant, step a) comprises the following steps:

-   -   a1′) preparing a support comprising at least γ-ketovaleric acid        and optionally at least one part of phosphorus,    -   a2′) impregnating the support obtained in step a1′) with an        impregnating solution comprising at least one element of group        VIB, at least one element of group VIII and optionally        phosphorus so as to obtain a catalyst precursor,    -   a3′) optionally, leaving the catalyst precursor obtained in step        a2′) to mature.

According to another variant, step a) comprises the following steps:

-   -   a1″) by co-impregnation, bringing a solution containing at least        one element of group VIB, at least one element of group VIII, at        least one organic compound containing oxygen and/or nitrogen        and/or sulphur, and optionally phosphorus into contact with a        support based on alumina or silica or silica-alumina so as to        obtain an impregnated support,    -   a2″) drying the impregnated support originating from step a1″)        at a temperature of less than 200° C., without calcining it        subsequently, in order to obtain a dried impregnated support,    -   a3″) bringing the dried impregnated support originating from        step a2″) into contact with a solution of an organic compound        containing oxygen and/or nitrogen and/or sulphur, identical to        or different from that used in step a1″) so as to obtain a        catalyst precursor,    -   a4″) optionally, leaving the catalyst precursor obtained in step        a3″) to mature, and at least one of the organic compounds in        step a1″) or in step a3″) is γ-ketovaleric acid.

According to a variant, when it is desired to prepare the catalystaccording to the invention starting from a regenerated catalyst, step a)of the preparation process comprises the following steps:

-   -   a1′″) impregnating a regenerated catalyst containing a support        based on alumina or silica or silica-alumina, at least one        component of an element of group VIB, at least one component of        an element of group VIII and optionally phosphorus with an        impregnating solution comprising at least γ-ketovaleric acid so        as to obtain a catalyst precursor,    -   a2′″) optionally, leaving the catalyst precursor obtained in        step a1′″) to mature.

According to a variant, the molar ratio of the γ-ketovaleric acid perelement(s) of group VIII is comprised between 0.1 and 5.0 mol/mol.

The invention also relates to the use of the catalyst according to theinvention or prepared by the preparation process according to theinvention in a process for hydrotreatment and/or hydrocracking ofhydrocarbon-containing cuts.

Hereinafter, the groups of chemical elements are given according to theCAS classification (CRC Handbook of Chemistry and Physics, publisher CRCPress, chief editor D. R. Lide, 81st edition, 2000-2001). For example,group VIII according to the CAS classification corresponds to the metalsof columns 8, 9 and 10 according to the new IUPAC classification.

By “hydrotreatment” is meant reactions including in particularhydrodesulphurization (HDS), hydrodenitrogenation (HDN) andhydrogenation of aromatics (HDA).

DETAILED DESCRIPTION OF THE INVENTION Catalyst

The catalyst according to the invention is an additive catalystcontaining at least γ-ketovaleric acid. More particularly, the catalystaccording to the invention comprises a support based on alumina orsilica or silica-alumina, at least one element of group VIII, at leastone element of group VIB and γ-ketovaleric acid.

The catalyst according to the invention may be a fresh catalyst, i.e. acatalyst that has not been used previously as a catalyst in a catalyticunit and in particular in hydrotreatment and/or hydrocracking.

The catalyst according to the invention may also be a rejuvenatedcatalyst. By rejuvenated catalyst is meant a catalyst that has been usedas a catalyst in a catalytic unit and in particular in hydrotreatmentand/or hydrocracking and that has undergone at least one step ofcalcination in order to burn off the coke (regeneration). Then at leastγ-ketovaleric acid is added to this regenerated catalyst in order toobtain the rejuvenated catalyst. This rejuvenated catalyst may containone or more other organic additive(s) which may be added before, afteror at the same time as the γ-ketovaleric acid.

The hydrogenating function of said catalyst, also called the activephase, is ensured by at least one element of group VIB and at least oneelement of group VIII.

The preferred elements of group VIB are molybdenum and tungsten. Thepreferred elements of group VIII are non-noble elements and inparticular cobalt and nickel. Advantageously, the hydrogenating functionis selected from the group comprising combinations of the elementscobalt-molybdenum, nickel-molybdenum, nickel-tungsten ornickel-cobalt-molybdenum, or nickel-molybdenum-tungsten.

In the case where a high activity in hydrodesulphurization, or inhydrodenitrogenation and in hydrogenation of aromatics is desired, thehydrogenating function is advantageously provided by the combination ofnickel and molybdenum; a combination of nickel and tungsten in thepresence of molybdenum may also be advantageous. In the case offeedstocks of the vacuum distillate type or heavier feedstocks,combinations of the cobalt-nickel-molybdenum type may advantageously beused.

The total content of elements of group VIB and group VIII isadvantageously greater than 6% by weight expressed as oxide with respectto the total weight of the catalyst. The content of the element of groupVIB is comprised between 5 and 40% by weight, preferably between 8 and35% by weight, and more preferably between 10 and 30% by weightexpressed as oxide of the metal of group VIB with respect to the totalweight of the catalyst.

The content of the element of group VIII is comprised between 1 and 10%by weight, preferably between 1.5 and 9% by weight, and more preferablybetween 2 and 8% by weight expressed as oxide of the metal of group VIIIwith respect to the total weight of the catalyst.

The molar ratio of an element of group VIII to an element of group VIBin the catalyst is preferably comprised between 0.1 and 0.8, preferablycomprised between 0.15 and 0.6 and even more preferably comprisedbetween 0.2 and 0.5.

The catalyst according to the invention advantageously also comprisesphosphorus as a dopant. The dopant is an element that is added, which initself does not have any catalytic character but which increases thecatalytic activity of the active phase.

The phosphorus content in said catalyst is preferably comprised between0.1 and 20% by weight expressed as P₂O₅, preferably between 0.2 and 15%by weight expressed as P₂O₅, and very preferably between 0.3 and 10% byweight expressed as P₂O₅.

The molar ratio of phosphorus to the element of group VIB in thecatalyst is greater than or equal to 0.05, preferably greater than orequal to 0.07, preferably comprised between 0.08 and 1, preferablycomprised between 0.08 and 0.7 and very preferably comprised between0.08 and 0.5.

The catalyst according to the invention may advantageously furthercontain at least one dopant selected from boron, fluorine and a mixtureof boron and fluorine.

When the catalyst contains boron, the boron content is preferablycomprised between 0.1 and 10% by weight expressed as boron oxide,preferably between 0.2 and 7% by weight, and very preferably comprisedbetween 0.2 and 5% by weight.

When the catalyst contains fluorine, the fluorine content is preferablycomprised between 0.1 and 10% by weight expressed as fluorine,preferably between 0.2 and 7% by weight, and very preferably comprisedbetween 0.2 and 5% by weight.

When the catalyst contains boron and fluorine, the total content ofboron and fluorine is preferably comprised between 0.1 and 10% by weightexpressed as boron oxide and fluorine, preferably between 0.2 and 7% byweight, and very preferably comprised between 0.2 and 5% by weight.

The catalyst according to the invention comprises a support based onalumina or silica or silica-alumina.

When the support of said catalyst is based on alumina, it contains morethan 50% of alumina, and generally it contains only alumina orsilica-alumina as defined below.

Preferably, the support comprises alumina, and preferably extrudedalumina. Preferably, the alumina is gamma alumina.

The alumina support advantageously has a total pore volume comprisedbetween 0.1 and 1.5 cm³·g⁻¹, preferably between 0.4 and 1.1 cm³·g⁻¹. Thetotal pore volume is measured by mercury porosimetry according tostandard ASTM D4284 with a wetting angle of 140°, as described in thework by Rouquerol F.; Rouquerol J.; Singh K. “Adsorption by Powders &Porous Solids: Principle, methodology and applications”, Academic Press,1999, for example by means of the model Autopore III™ apparatus with thetrade mark Micromeritics™.

The specific surface area of the alumina support is advantageouslycomprised between 5 and 400 m²·g⁻¹, preferably between 10 and 350m²·g⁻¹, more preferably between 40 and 350 m²·g⁻¹. The specific surfacearea is determined in the present invention by the BET method accordingto standard ASTM D3663; this method is described in the same work citedabove.

In another preferred case, the support of said catalyst is asilica-alumina containing at least 50% by weight of alumina. The silicacontent of the support is at most 50% by weight, most often less than orequal to 45% by weight, preferably less than or equal to 40%.

The sources of silicon are well known to a person skilled in the art. Byway of example silicic acid, silica in the form of powder or incolloidal form (silica sol), and tetraethylorthosilicate Si(OEt)₄ may bementioned.

When the support of said catalyst is based on silica, it contains morethan 50% by weight of silica, and generally it only contains silica.

According to a particularly preferred variant, the support consists ofalumina, silica or silica-alumina.

The support may also advantageously further contain from 0.1 to 50% byweight of zeolite. In this case, all the sources of zeolite and all theassociated methods of preparation known to a person skilled in the artmay be incorporated. Preferably, the zeolite is selected from the groupFAU, BEA, ISV, IWR, IWW, MEI, UWY, and preferably the zeolite isselected from the group FAU and BEA, such as zeolite Y and/or beta.

In certain particular cases, the support may also contain at least onepart of the VIB and VIII metal (metals), and/or at least one part of thedopant(s) including phosphorus and/or at least one part of the organiccompound(s) containing oxygen (γ-ketovaleric acid or other) and/ornitrogen and/or sulphur that were introduced outside of theimpregnations (introduced for example during preparation of thesupport).

The support is advantageously in the form of beads, extrudates, pellets,or irregular, non-spherical agglomerates, the specific form of which mayresult from a crushing step.

The catalyst according to the invention also comprises γ-ketovalericacid. The γ-ketovaleric acid corresponds to the following formula:

The source of γ-ketovaleric acid can be from the conventional chemicalindustry with generally high levels of purity. The acid can alsooriginate from biomass processing, the product preferably containing amajority of γ-ketovaleric acid being purified or not before use. By wayof example, there may be mentioned the Biofine process (D. J. Hayes, J.Ross, M. H. B. Hayes, S. Fitzpatrick, Bioref. Ind. Proc. Prod., 1,139-164, 2006) which makes it possible, starting from lignocellulose, toproduce before purification a mixture containing at least 50% by weightof γ-ketovaleric acid, one of the major by-products being formic acid.

The presence of γ-ketovaleric acid on the catalyst makes it possible toobserve an increase in activity with respect to the catalysts withoutadditives and the known dried catalysts with additives. The content ofγ-ketovaleric acid on the catalyst according to the invention iscomprised between 1 and 35% by weight, preferably between 2 and 30% byweight, and more preferably between 3 and 25% by weight with respect tothe total weight of the catalyst. During preparation of the catalyst,the step or steps of drying following introduction of the acid is (are)carried out at a temperature of less than 200° C. so as preferably toretain at least 30%, preferably at least 50%, and very preferably atleast 70% of the quantity of acid introduced, calculated on the basis ofthe carbon remaining on the catalyst.

The catalyst according to the invention may comprise, in addition toγ-ketovaleric acid, another organic compound or a group of organiccompounds known for their role as additives. The function of theadditives is to increase the catalytic activity, with respect to thecatalysts without additives. More particularly, the catalyst accordingto the invention may further comprise one or more organic compoundscontaining oxygen other than γ-ketovaleric acid and/or one or moreorganic compounds containing nitrogen and/or one or more organiccompounds containing sulphur. Preferably, the catalyst according to theinvention may further comprise one or more organic compounds containingoxygen other than γ-ketovaleric acid, and/or one or more organiccompounds containing nitrogen. Preferably, the organic compound containsat least 2 carbon atoms and at least one oxygen and/or nitrogen atom.

Generally, the organic compound is selected from a compound comprisingone or more chemical functions selected from a carboxyl, alcohol, thiol,thioether, sulphone, sulphoxide, ether, aldehyde, ketone, ester,carbonate, amine, nitrile, imide, oxime, urea and amide function.Preferably, the organic compound is selected from a compound comprisingtwo alcohol functions and/or two carboxyl functions and/or two esterfunctions and/or at least one amide function.

The organic compound containing oxygen may be one or more selected fromthe compounds comprising one or more chemical functions selected from acarboxyl, alcohol, ether, aldehyde, ketone, ester or carbonate function.By way of example, the organic compound containing oxygen may be one ormore selected from the group constituted by ethylene glycol, diethyleneglycol, triethylene glycol, a polyethylene glycol (with a molecularweight comprised between 200 and 1500 g/mol), propylene glycol,2-butoxyethanol, 2-(2-butoxyethoxy)ethanol, 2-(2-methoxyethoxy)ethanol,triethyleneglycol dimethyl ether, glycerol, acetophenone,2,4-pentanedione, pentanone, acetic acid, maleic acid, malic acid,malonic acid, malic acid, oxalic acid, gluconic acid, tartaric acid,citric acid, a C₁-C₄ dialkyl succinate, methyl acetoacetate, a lactone,dibenzofuran, a crown ether, orthophthalic acid, glucose and propylenecarbonate.

The organic compound containing nitrogen may be one or more selectedfrom the compounds comprising one or more chemical functions selectedfrom an amine or nitrile function. By way of example, the organiccompound containing nitrogen may be one or more selected from the groupconstituted by ethylenediamine, diethylenetriamine,hexamethylenediamine, triethylenetetramine, tetraethylenepentamine,pentaethylenehexamine, acetonitrile, octylamine, guanidine or acarbazole.

The organic compound containing oxygen and nitrogen may be one or moreselected from the compounds comprising one or more chemical functionsselected from a carboxylic acid, alcohol, ether, aldehyde, ketone,ester, carbonate, amine, nitrile, imide, amide, urea or oxime function.By way of example, the organic compound containing oxygen and nitrogenmay be one or more selected from the group constituted by1,2-cyclohexanediaminetetraacetic acid, monoethanolamine (MEA),N-methylpyrrolidone, dimethylformamide, ethylenediaminetetraacetic acid(EDTA), alanine, glycine, nitrilotriacetic acid (NTA),N-(2-hydroxyethyl)ethylenediamine-N,N′,N′-triacetic acid (HEDTA),diethylenetriaminepentaacetic acid (DTPA), tetramethylurea, glutamicacid, dimethylglyoxime, bicine or tricine, or a lactam.

The organic compound containing sulphur may be one or more selected fromthe compounds comprising one or more chemical functions selected from athiol, thioether, sulphone or sulphoxide function. By way of example,the organic compound containing sulphur may be one or more selected fromthe group constituted by thioglycolic acid,2-hydroxy-4-methylthiobutanoic acid, a sulphonated derivative of abenzothiophene or a sulphoxidized derivative of a benzothiophene.Preferably, the organic compound contains oxygen, and preferably it isselected from triethylene glycol, diethylene glycol,ethylenediaminetetraacetic acid (EDTA), maleic acid, citric acid,dimethylformamide, bicine, or tricine.

When it (they) is/are present, the content of organic compound(s) withadditive function (other than γ-ketovaleric acid) containing oxygenand/or nitrogen and/or sulphur on the catalyst according to theinvention is comprised between 1 and 30% by weight, preferably between1.5 and 25% by weight, and more preferably between 2 and 20% by weightwith respect to the total weight of the catalyst.

Preparation Process

The catalyst according to the invention may be prepared by any processfor the preparation of a supported catalyst with an organic compound asadditive known to a person skilled in the art.

The catalyst according to the invention may be prepared by a preparationprocess comprising the following steps:

-   -   a) bringing at least one component of an element of group VIB,        at least one component of an element of group VIII,        γ-ketovaleric acid and optionally phosphorus into contact with a        support based on alumina or silica or silica-alumina, or        bringing a regenerated catalyst containing a support based on        alumina or silica or silica-alumina, at least one component of        an element of group VIB, at least one component of an element of        group VIII and optionally phosphorus into contact with        γ-ketovaleric acid, so as to obtain a catalyst precursor,    -   b) drying said catalyst precursor originating from step a) at a        temperature of less than 200° C., without calcining it        subsequently.

First, the process for the preparation of a fresh catalyst will bedescribed, and after that, the process for the preparation of arejuvenated catalyst.

Process for the Preparation of a Fresh Catalyst

The contacting step a) comprises several embodiments, which differ inparticular by the time of introduction of γ-ketovaleric acid, which maybe carried out either at the same time as impregnation of the metals(co-impregnation), or after impregnation of the metals(post-impregnation), or finally before impregnation of the metals(pre-impregnation). Moreover, the contacting step may combine at leasttwo embodiments, for example co-impregnation and post-impregnation.These various embodiments will be described later. Each embodiment,alone or in combination, may take place in one or more steps.

It is important to emphasize that during its preparation process, thecatalyst according to the invention does not undergo calcination afterintroduction of the γ-ketovaleric acid or any other organic compoundcontaining oxygen and/or nitrogen and/or sulphur in order to preserve,at least partly, the γ-ketovaleric acid or any other organic compound inthe catalyst. By calcination is meant here a heat treatment under a gascontaining air or oxygen at a temperature greater than or equal to 200°C.

However, the catalyst precursor may undergo a calcining step before theintroduction of γ-ketovaleric acid or any other organic compoundcontaining oxygen and/or nitrogen and/or sulphur, in particular afterimpregnation of the elements of group VIB and VIII (post-impregnation)optionally in the presence of phosphorus and/or of another dopant orduring regeneration of a catalyst that has already been used. Thehydrogenating function comprising the elements of group VIB and groupVIII of the catalyst according to the invention, also called the activephase, is then in an oxide form.

According to another variant, the catalyst precursor does not undergo acalcining step after impregnation of the elements of group VIB and VIII(post-impregnation), it is simply dried. The hydrogenating functioncomprising the elements of group VIB and group VIII of the catalystaccording to the invention, also called the active phase, is not then inan oxide form.

Whatever the embodiment, the contacting step a) generally comprises atleast one step of impregnation, preferably a step of dry impregnation,in which the support is impregnated with an impregnating solutioncomprising at least one element of group VIB, at least one element ofgroup VIII, and optionally phosphorus. In the case of co-impregnation,described in detail below, this impregnating solution further comprisesat least γ-ketovaleric acid. The elements of group VIB and group VIIIare generally introduced by impregnation, preferably by dry impregnationor by impregnation with excess solution. Preferably, all of the elementsof group VIB and group VIII are introduced by impregnation, preferablyby dry impregnation, regardless of the embodiment.

The elements of group VIB and group VIII may also be introduced partlyduring forming said support at the time of mixing with at least onealumina gel selected as matrix, the rest of the hydrogenating elementsthen being introduced subsequently by impregnation. Preferably, when theelements of group VIB and group VIII are introduced partly at the timeof mixing, the proportion of the element of group VIB introduced duringthis step is less than 5% by weight of the total quantity of the elementof group VIB introduced on the final catalyst.

Preferably, the element of group VIB is introduced at the same time asthe element of group VIII, regardless of the method of introduction.

The molybdenum precursors that may be used are well known to a personskilled in the art. For example, among the sources of molybdenum, theoxides and hydroxides, the molybdic acids and salts thereof can be used,in particular the ammonium salts such as ammonium molybdate, ammoniumheptamolybdate, phosphomolybdic acid (H₃PMo₁₂O₄₀) and salts thereof, andoptionally silicomolybdic acid (H₄SiMo₁₂O₄₀) and salts thereof. Thesources of molybdenum may also be heteropoly compounds of the Keggin,lacunar Keggin, substituted Keggin, Dawson, Anderson, or Strandbergtype, for example. Molybdenum trioxide and the heteropolyanions of theStrandberg, Keggin, lacunar Keggin or substituted Keggin type arepreferably used.

The tungsten precursors that may be used are also well known to a personskilled in the art. For example, among the sources of tungsten, theoxides and hydroxides, the tungstic acids and salts thereof can be used,in particular the ammonium salts such as ammonium tungstate, ammoniummetatungstate, phosphotungstic acid and salts thereof, and optionallysilicotungstic acid (H₄SiW₁₂O₄₀) and salts thereof. The sources oftungsten may also be heteropoly compounds of the Keggin, lacunar Keggin,substituted Keggin, or Dawson type, for example. The oxides and theammonium salts such as ammonium metatungstate or the heteropolyanions ofthe Keggin, lacunar Keggin or substituted Keggin type are preferablyused.

The precursors of the elements of group VIII that may be used areadvantageously selected from the oxides, hydroxides, hydroxycarbonates,carbonates and nitrates of the elements of group VIII, for examplenickel hydroxycarbonate, cobalt carbonate or hydroxide are preferablyused.

Phosphorus, when it is present, may be introduced wholly or partly byimpregnation. Preferably, it is introduced by impregnation, preferablydry impregnation, using a solution containing the precursors of theelements of group VIB and group VIII.

Said phosphorus may advantageously be introduced alone or in a mixturewith at least one of the elements of group VIB and group VIII, duringany of the steps for impregnation of the hydrogenating function if thisis introduced in several goes. Said phosphorus may also be introduced,wholly or partly, during the impregnation of γ-ketovaleric acid if thisis introduced separately from the hydrogenating function (the case ofpost- and pre-impregnation described later), in the presence or absenceof an organic compound other than γ-ketovaleric acid containing oxygenand/or nitrogen and/or sulphur. It may also be introduced duringsynthesis of the support, at any step of the synthesis thereof. It maythus be introduced before, during or after mixing of the alumina gelmatrix selected, such as for example and preferably the aluminaprecursor aluminium oxyhydroxide (boehmite).

The preferred phosphorus precursor is orthophosphoric acid H₃PO₄, butsalts and esters thereof such as the ammonium phosphates are alsosuitable. Phosphorus may also be introduced at the same time as theelement(s) of group VIB in the form of heteropolyanions of the Keggin,lacunar Keggin, substituted Keggin or Strandberg type.

The γ-ketovaleric acid is advantageously introduced into an impregnatingsolution which, depending on the preparation process, may be the samesolution or a different solution from that containing the elements ofgroup VIB and VIII, in a total quantity corresponding to:

-   -   a molar ratio of γ-ketovaleric acid to the element(s) of group        VIB of the catalyst precursor comprised between 0.2 and 2.0        mol/mol, preferably comprised between 0.3 and 1.7 mol/mol,        preferably comprised between 0.5 and 1.5 mol/mol and very        preferably comprised between 0.8 and 1.2 mol/mol, calculated on        the basis of the components introduced into the impregnating        solution(s), and    -   a molar ratio of γ-ketovaleric acid to the element(s) of group        VIII of the catalyst precursor comprised between 0.1 and 5.0        mol/mol, preferably comprised between 0.5 and 4.0 mol/mol,        preferably comprised between 1.0 and 3.0 mol/mol and very        preferably comprised between 1.5 and 3.0 mol/mol, calculated on        the basis of the components introduced into the impregnating        solution(s).

Any impregnating solution described in the present invention maycomprise any polar solvent known to a person skilled in the art. Saidpolar solvent used is advantageously selected from the group formed bymethanol, ethanol, water, phenol, cyclohexanol, used alone or in amixture. Said polar solvent may also be advantageously selected from thegroup formed by propylene carbonate, DMSO (dimethylsulphoxide),N-methylpyrrolidone (NMP) or sulpholane, used alone or in a mixture.Preferably, a polar protic solvent is used. A list of the usual polarsolvents as well as their dielectric constant may be found in the book“Solvents and Solvent Effects in Organic Chemistry” C. Reichardt,Wiley-VCH, 3rd edition, 2003, pages 472-474. Very preferably, thesolvent used is water or ethanol, and particularly preferably thesolvent is water. In a possible embodiment, the solvent may be absentfrom the impregnating solution.

When the catalyst further comprises a dopant selected from boron,fluorine or a mixture of boron and fluorine, introduction of this dopantor these dopants may be done in the same way as the introduction ofphosphorus at various steps of the preparation and in various ways. Saiddopant may advantageously be introduced alone or in a mixture with atleast one of the elements of group VIB and group VIII, during any of thesteps of impregnation of the hydrogenating function if this isintroduced in several goes. Said dopant may also be introduced, whollyor partly, during impregnation of γ-ketovaleric acid if this isintroduced separately from the hydrogenating function (the case of post-and pre-impregnation, described later), in the presence or absence of anorganic compound other than γ-ketovaleric acid containing oxygen and/ornitrogen and/or sulphur. It may also be introduced from synthesis of thesupport onwards, at any step of the synthesis thereof. It may thus beintroduced before, during or after mixing of the alumina gel matrixselected, such as for example and preferably the alumina precursoraluminium oxyhydroxide (boehmite).

Said dopant, when present, is advantageously introduced in a mixturewith the precursor(s) of the elements of group VIB and group VIII,wholly or partly on the formed support by dry impregnation of saidsupport using a solution, preferably aqueous, containing the precursorsof the metals, the phosphorus precursor and the precursor(s) of thedopant(s) (and also containing γ-ketovaleric acid in the co-impregnationembodiment).

The boron precursors may be boric acid, orthoboric acid H₃BO₃, ammoniumdiborate or pentaborate, boron oxide, boric esters. Boron may beintroduced for example by means of a solution of boric acid in awater/alcohol mixture or also in a water/ethanolamine mixture.Preferably the boron precursor, if boron is introduced, is orthoboricacid.

The fluorine precursors that may be used are well known to a personskilled in the art. For example, the fluoride anions may be introducedin the form of hydrofluoric acid or salts thereof. These salts areformed with alkali metals, ammonium or an organic compound. In thelatter case, the salt is advantageously formed in the reaction mixtureby reaction between the organic compound and hydrofluoric acid. Fluorinemay be introduced for example by impregnation of an aqueous solution ofhydrofluoric acid, or ammonium fluoride or ammonium bifluoride.

When the catalyst further comprises an additional additive (in additionto γ-ketovaleric acid) or a group of additional additives selected froman organic compound other than γ-ketovaleric acid containing oxygenand/or nitrogen and/or sulphur, this may be introduced in theimpregnating solution in step a).

The molar ratio of organic compound(s) containing oxygen and/or nitrogenand/or sulphur to element(s) of group VIB on the catalyst is comprisedbetween 0.05 and 5 mol/mol, preferably comprised between 0.1 and 4mol/mol, preferably comprised between 0.2 and 3 mol/mol, calculated onthe basis of the components introduced into the impregnatingsolution(s).

The molar ratio of organic compound(s) containing oxygen and/or nitrogenand/or sulphur to γ-ketovaleric acid is comprised between 0.05 and 5mol/mol, preferably comprised between 0.1 and 4 mol/mol, more preferablycomprised between 0.2 and 3 mol/mol, calculated on the basis of thecomponents introduced into the impregnating solution(s).

Advantageously, after each impregnating step, the impregnated support isleft to mature. Maturation allows the impregnating solution to dispersehomogeneously within the support.

Any maturation step described in the present invention is advantageouslycarried out at atmospheric pressure, in a water-saturated atmosphere andat a temperature comprised between 17° C. and 50° C., and preferably atambient temperature. Generally a maturation time comprised between tenminutes and forty-eight hours and preferably comprised between thirtyminutes and five hours is sufficient. Longer times are not excluded, butdo not necessarily provide any improvement.

According to step b) of the preparation process according to theinvention, the catalyst precursor obtained in step a), optionallymatured, is subjected to a drying step at a temperature of less than200° C. without a subsequent calcining step.

Any drying step subsequent to the introduction of γ-ketovaleric aciddescribed in the present invention is carried out at a temperature ofless than 200° C., preferably comprised between 50 and 180° C.,preferably between 70 and 150° C. and very preferably between 75 and130° C.

The drying step is advantageously carried out by any technique known toa person skilled in the art. It is advantageously carried out atatmospheric pressure or at reduced pressure. Preferably this step iscarried out at atmospheric pressure. It is advantageously carried out ina transversed bed using air or any other hot gas. Preferably, whendrying is carried out in a fixed bed, the gas used is either air, or aninert gas such as argon or nitrogen. Very preferably, drying is carriedout in a transversed bed in the presence of nitrogen and/or air.Preferably, the drying step is of short duration, comprised between 5minutes and 4 hours, preferably between 30 minutes and 4 hours and verypreferably between 1 hour and 3 hours. Drying is then carried out so aspreferably to retain at least 30% of the γ-ketovaleric acid introducedduring an impregnation step, preferably this quantity is greater than50% and even more preferably greater than 70%, calculated on the basisof the carbon remaining on the catalyst. When an organic compound otherthan γ-ketovaleric acid containing oxygen and/or nitrogen and/or sulphuris present, the drying step is carried out so as preferably to retain atleast 30%, preferably at least 50%, and very preferably at least 70% ofthe quantity introduced, calculated on the basis of the carbon remainingon the catalyst.

At the end of the drying step b), a dried catalyst is obtained, which isnot subjected to any subsequent calcining step.

Co-Impregnation

According to a first embodiment of step a) of the process for thepreparation of the (fresh) catalyst, said components of the elements ofgroup VIB, of the elements of group VIII, of γ-ketovaleric acid andoptionally phosphorus are deposited on said support, by one or moreco-impregnation steps, i.e. said components of the elements of groupVIB, of the elements of group VIII, of γ-ketovaleric acid and optionallyphosphorus are introduced simultaneously into said support(“co-impregnation”). According to a variant, step a) is the followingstep:

-   -   a′) impregnating a support based on alumina or silica or        silica-alumina with at least one solution containing at least        one element of group VIB, at least one element of group VIII, of        γ-ketovaleric acid and optionally phosphorus so as to obtain a        catalyst precursor.

The co-impregnation step or steps is (are) preferably carried out by dryimpregnation or by impregnation with excess solution. When this firstembodiment comprises the utilization of several co-impregnation steps,each co-impregnation step is preferably followed by an intermediatedrying step at a temperature of less than 200° C., advantageouslycomprised between 50 and 180° C., preferably between 70 and 150° C.,very preferably between 75 and 130° C., optionally observing a period ofmaturation between impregnation and drying.

Very preferably, during preparation by co-impregnation, the elements ofgroup VIB and group VIII, of γ-ketovaleric acid, optionally phosphorus,optionally another dopant selected from boron and/or fluorine andoptionally an organic compound other than γ-ketovaleric acid containingoxygen and/or nitrogen and/or sulphur are introduced in step a) entirelyafter the forming of said support, by dry impregnation of said supportusing an aqueous impregnating solution containing the precursors of theelements of group VIB and group VIII, of γ-ketovaleric acid, optionallythe phosphorus precursor, optionally the dopant precursor selected fromboron and/or fluorine and optionally the organic compound containingoxygen and/or nitrogen and/or sulphur.

Post-Impregnation

According to a second embodiment of step a) of the process for thepreparation of the (fresh) catalyst according to the invention, at leastγ-ketovaleric acid is brought into contact with a dried and optionallycalcined impregnated support comprising at least one component of anelement of group VIB, at least one component of an element of group VIIIand optionally phosphorus, said support being based on alumina or silicaor silica-alumina, so as to obtain a catalyst precursor.

This second embodiment is a preparation by “post-impregnation” ofγ-ketovaleric acid. This is carried out for example by dry impregnation.

According to this second embodiment, the contacting according to step a)comprises the following successive steps, which will be described indetail later:

-   -   a1) impregnating a support based on alumina or silica or        silica-alumina with at least one solution containing at least        one element of group VIB, at least one element of group VIII and        optionally phosphorus in order to obtain an impregnated support,    -   a2) drying the impregnated support obtained in step a1) at a        temperature of less than 200° C. in order to obtain a dried        impregnated support, and optionally calcining the dried        impregnated support in order to obtain a calcined impregnated        support,    -   a3) impregnating the dried and optionally calcined impregnated        support obtained in step a2) with an impregnating solution        comprising at least γ-ketovaleric acid so as to obtain a        catalyst precursor,    -   a4) optionally, leaving the catalyst precursor obtained in step        a3) to mature.

In step a1) of the embodiment utilizing post-impregnation, theintroduction of the elements of group VIB and group VIII and optionallyphosphorus on the support may advantageously be carried out by one ormore impregnations with excess solution on the support, or preferably byone or more dry impregnations, and preferably by a single dryimpregnation of said support, using solution(s), preferably aqueous,containing the precursor or precursors of metals and preferably thephosphorus precursor.

When several impregnation steps are carried out, each impregnation stepis preferably followed by an intermediate drying step at a temperatureof less than 200° C., advantageously between 50 and 180° C., preferablybetween 70 and 150° C., very preferably between 75 and 130° C., andoptionally observing a period of maturation between impregnation anddrying. Each intermediate drying step, prior to the introduction ofγ-ketovaleric acid, may be followed by a calcining step under theconditions described below for step a2).

Very preferably, during preparation by post-impregnation, the elementsof group VIB and group VIII and optionally phosphorus, optionallyanother dopant selected from boron and/or fluorine and optionally anorganic compound other than γ-ketovaleric acid containing oxygen and/ornitrogen and/or sulphur are introduced in step a1) entirely after theforming of said support, by dry impregnation of said support using anaqueous impregnating solution containing the precursors of the elementsof group VIB and group VIII, the phosphorus precursor, and optionallythe dopant precursor selected from boron and/or fluorine and optionallythe organic compound other than γ-ketovaleric acid containing oxygenand/or nitrogen and/or sulphur.

According to another variant, the elements of group VIB and group VIIIand optionally phosphorus, optionally another dopant selected from boronand/or fluorine and optionally an organic compound other thanγ-ketovaleric acid containing oxygen and/or nitrogen and/or sulphur maybe introduced in step a1) successively by means of several impregnatingsolutions containing one or more of the components.

Advantageously, the impregnated support obtained in step a1) is left tomature under the conditions described above for maturation.

According to step a2), the impregnated support obtained in step a1) isdried at a temperature of less than 200° C. in order to obtain animpregnated support, dried under the drying conditions described above.

Optionally, the dried impregnated support may then undergo calcining.Calcining is generally carried out at a temperature comprised between200° C. and 900° C., preferably comprised between 250° C. and 750° C.The calcination time is generally comprised between 0.5 hours and 16hours, preferably between 1 hour and 5 hours.

It is generally carried out under air. Calcining makes it possible toconvert the precursors of the group VIB and group VIII metals to oxides.

According to step a3), the dried impregnated support obtained in stepa2) is impregnated with an impregnating solution comprising at leastγ-ketovaleric acid so as to obtain a catalyst precursor.

The γ-ketovaleric acid may advantageously be deposited in one or moresteps either by impregnation in excess, or by dry impregnation, or byany other means known to a person skilled in the art. Preferably, theγ-ketovaleric acid is introduced by dry impregnation, in the presence orabsence of a solvent as described above.

Preferably, the solvent in the impregnating solution used in step a3) iswater, which facilitates implementation on an industrial scale.

The γ-ketovaleric acid is advantageously introduced into theimpregnating solution in step a3) with the molar ratios per element ofgroup VIB or of group VIII described above.

When in addition it is desired to introduce an additional additive (inaddition to γ-ketovaleric acid) or a group of additional additivesselected from an organic compound containing oxygen and/or nitrogenand/or sulphur, this may be introduced in the impregnating solution instep a1) and/or in the impregnating solution in step a3) or by anadditional impregnation step at any time in the preparation processbefore the final drying in step b), it being understood that a calciningstep is not carried out after its introduction. This compound isintroduced in the proportions described above.

According to step a4), optionally the catalyst precursor obtained instep a3) is left to mature, under the maturation conditions describedabove.

According to step b) of the preparation process according to theinvention, the catalyst precursor that was optionally matured in stepa4) is subjected to a step of drying at a temperature of less than 200°C. without a subsequent calcining step, as described above.

Pre-Impregnation

According to a third embodiment of step a) of the process for thepreparation of the (fresh) catalyst according to the invention, at leastone component of an element of group VIB, at least one component of anelement of group VIII, and optionally phosphorus are brought intocontact with the support based on alumina or silica or silica-aluminathat contains γ-ketovaleric acid so as to obtain a catalyst precursor.This third embodiment is a preparation by “pre-impregnation” ofγ-ketovaleric acid. This is carried out for example by dry impregnation.

According to this third embodiment, the contacting according to step a)comprises the following successive steps, which will be described indetail later:

-   -   a1′) preparing a support comprising at least γ-ketovaleric acid        and optionally at least one part of phosphorus,    -   a2′) impregnating the support obtained in step a1′) with an        impregnating solution comprising at least one element of group        VIB, at least one element of group VIII and optionally        phosphorus so as to obtain a catalyst precursor,    -   a3′) optionally, leaving the catalyst precursor obtained in step        a2′) to mature.

In step a1′) of the embodiment utilizing pre-impregnation, a support isprepared comprising at least γ-ketovaleric acid and optionally at leastone part of phosphorus. The γ-ketovaleric acid may be introduced at anytime in the preparation of the support, and preferably during forming orby impregnation on a support already formed.

If introduction of γ-ketovaleric acid on the previously formed supportis selected, the latter may be carried out as is indicated for step a3)of post-impregnation. It will then be followed by an optional maturationstep and by drying at a temperature of less than 200° C. under theconditions of maturation and drying as described above.

If introduction during forming is selected, preferably said forming iscarried out by mixing-extrusion, by pelletization, by the oil-dropmethod, by granulation with a rotating plate or by any other method wellknown to a person skilled in the art. Very preferably, said forming iscarried out by mixing-extrusion, and the γ-ketovaleric acid may beintroduced at any time during mixing-extrusion. The formed materialobtained at the end of the forming step then advantageously undergoes astep of heat treatment at a temperature such that at least a proportionof the γ-ketovaleric acid remains present.

The same applies to the phosphorus optionally present in said support instep a1′). Phosphorus may be introduced at any time in the preparationof the support, and preferably during forming or by impregnation on asupport already formed as described above. If only phosphorus isintroduced during forming, i.e. without γ-ketovaleric acid itself thenintroduced by impregnation, the calcination temperature following itsintroduction may then advantageously be carried out at a temperature ofless than 1,000° C.

In step a2′) of the embodiment utilizing pre-impregnation, theintroduction of the elements of group VIB and group VIII and optionallyphosphorus may advantageously be carried out by one or moreimpregnations in excess solution on the support, or preferably by one ormore dry impregnations, and preferably by a single dry impregnation ofsaid support, using solution(s), preferably aqueous, containing theprecursor or precursors of metals and optionally the phosphorusprecursor.

Advantageously, the catalyst precursor obtained in step a2′) is left tomature under the maturation conditions described above.

When in addition it is desired to introduce an additional additive (inaddition to γ-ketovaleric acid) or a group of additional additivesselected from an organic compound containing oxygen and/or nitrogenand/or sulphur, this may be introduced into the support in step a1′)during forming or by impregnation, and/or into the impregnating solutionin step a2′) or by an additional impregnation step at any time in thepreparation process before the final drying in step b), it beingunderstood that a calcining step is not carried out after itsintroduction.

The three embodiments described above may be carried out alone asdescribed, or in a mixture in order to give rise to other hybrid methodsof preparation depending on the technical and practical constraints.

According to another alternative embodiment, the contacting according tostep a) combines at least two methods of contacting, for exampleco-impregnation of an organic compound and post-impregnation of anorganic compound, which may be identical to or different from that usedfor co-impregnation, given that at least one of the organic compounds isγ-ketovaleric acid.

According to this alternative embodiment, the contacting according tostep a) comprises the following successive steps:

-   -   a1″) by co-impregnation, bringing a solution containing at least        one element of group VIB, at least one element of group VIII, at        least one organic compound containing oxygen and/or nitrogen        and/or sulphur, and optionally phosphorus into contact with a        support based on alumina or silica or silica-alumina so as to        obtain an impregnated support,    -   a2″) drying the impregnated support originating from step a1″)        at a temperature of less than 200° C., without calcining it        subsequently, in order to obtain a dried impregnated support,    -   a3″) bringing the dried impregnated support originating from        step a2″) into contact with a solution of an organic compound        containing oxygen and/or nitrogen and/or sulphur, identical to        or different from that used in step a1″) so as to obtain a        catalyst precursor,    -   a4″) optionally, leaving the catalyst precursor obtained in step        a3″) to mature. and at least one of the organic compounds in        step a1″) or in step a3″) is γ-ketovaleric acid.

The operating conditions described above are of course applicable in thecontext of this last-mentioned embodiment.

Process for the Preparation of a Rejuvenated Catalyst

The catalyst according to the invention may be a rejuvenated catalyst.This catalyst may be prepared by the preparation process comprising thefollowing steps:

-   -   a) bringing a regenerated catalyst containing a support based on        alumina or silica or silica-alumina, at least one component of        an element of group VIB, at least one component of an element of        group VIII and optionally phosphorus into contact with        γ-ketovaleric acid so as to obtain a catalyst precursor,    -   b) drying said catalyst precursor originating from step a) at a        temperature of less than 200° C., without calcining it        subsequently.

According to step a), a regenerated catalyst is brought into contactwith γ-ketovaleric acid, so as to obtain a catalyst precursor. Theregenerated catalyst is a catalyst that has been used as a catalyst in acatalytic unit and in particular in hydrotreatment and/or hydrocrackingand that has undergone at least one step of calcining, in order to burnoff the coke (regeneration). Regeneration allows combustion of thecarbon deposited on the catalyst during its industrial use. It may becarried out by any means known to a person skilled in the art.Regeneration is generally carried out at temperatures comprised between350 and 550° C., and most often between 400 and 520° C., or between 420and 520° C., or between 450 and 520° C., temperatures of less than 500°C. often being advantageous.

The regenerated catalyst contains a support based on alumina or silicaor silica-alumina, at least one component of an element of group VIB, atleast one component of an element of group VIII and optionallyphosphorus in the respective proportions given above. Followingregeneration (calcining step), the hydrogenating function comprising theelements of group VIB and group VIII of the regenerated catalyst is inan oxide form. It may also contain dopants other than phosphorus, asdescribed above.

According to this embodiment, the contacting according to step a)comprises the following successive steps:

-   -   a1′″) impregnating a regenerated catalyst containing a support        based on alumina or silica or silica-alumina, at least one        component of an element of group VIB, at least one component of        an element of group VIII and optionally phosphorus with an        impregnating solution comprising at least γ-ketovaleric acid so        as to obtain a catalyst precursor,    -   a2′″) optionally, leaving the catalyst precursor obtained in        step a1′″) to mature.

Preferably, the contacting in step a) is carried out by impregnation ofthe regenerated catalyst with an impregnating solution comprising atleast γ-ketovaleric acid so as to obtain a catalyst precursor.

The γ-ketovaleric acid may advantageously be deposited in one or moresteps either by impregnation in excess, or by dry impregnation, or byany other means known to a person skilled in the art. Preferably, theγ-ketovaleric acid is introduced by dry impregnation, in the presence orabsence of a solvent as described above.

Preferably, the solvent in the impregnating solution used is water,which facilitates implementation on an industrial scale.

The γ-ketovaleric acid is advantageously introduced into theimpregnating solution with the molar ratios per element of group VIB orof group VIII described above.

When in addition it is desired to introduce an additional additive (inaddition to the γ-ketovaleric acid) or a group of additional additivesselected from an organic compound containing oxygen and/or nitrogenand/or sulphur, this may be introduced in the impregnating solution instep a1′″) or by an additional impregnation step at any time in thepreparation process before the final drying in step b), it beingunderstood that a calcining step is not carried out after itsintroduction. This compound is introduced in the proportions describedabove.

According to step a2″″), optionally the catalyst precursor obtained instep a1′″) is left to mature, under the maturation conditions describedabove.

According to step b) of the preparation process according to theinvention, the catalyst precursor that has optionally been maturedduring step a2′″) is subjected to a step of drying at a temperature ofless than 200° C. without a subsequent calcining step, as describedabove.

Sulphurization

Before it is used for the hydrotreatment and/or hydrocracking reaction,it is advantageous to convert the dried catalyst obtained according toany one of the methods of introduction described in the presentinvention to a sulphurized catalyst in order to form its active species.This activation or sulphurization step is carried out by the methodswell known to a person skilled in the art, and advantageously under asulpho-reducing atmosphere in the presence of hydrogen and hydrogensulphide.

At the end of step b) according to the various methods of preparation ofthe method according to the invention, said catalyst obtained istherefore advantageously subjected to a sulphurization step, without anintermediate calcining step.

Said dried catalyst is advantageously sulphurized ex situ or in situ.The sulphurization agents are H₂S gas or any other compound containingsulphur used for the activation of hydrocarbon feedstocks forsulphurization of the catalyst. Said compounds containing sulphur areadvantageously selected from the alkyl disulphides such as for exampledimethyl disulphide (DMDS), the alkyl sulphides, such as for exampledimethyl sulphide, the thiols such as for example n-butylmercaptan (or1-butanethiol), the polysulphide compounds of the tert-nonylpolysulphidetype, or any other compound known to a person skilled in the art forobtaining good sulphurization of the catalyst. Preferably the catalystis sulphurized in situ in the presence of a sulphurization agent and ahydrocarbon-containing feedstock. Very preferably the catalyst issulphurized in situ in the presence of a hydrocarbon-containingfeedstock to which dimethyl disulphide has been added.

Hydrotreatment and/or Hydrocracking Process

Finally, the invention also relates to the use of the catalyst accordingto the invention or prepared by the preparation process according to theinvention in processes for hydrotreatment and/or hydrocracking ofhydrocarbon-containing cuts.

The catalyst according to the invention, which preferably has undergonea sulphurization step beforehand, is used advantageously for thereactions of hydrotreatment and/or hydrocracking ofhydrocarbon-containing feedstocks such as petroleum cuts, cutsoriginating from coal or the hydrocarbons produced from natural gas,optionally in mixtures, or from a hydrocarbon-containing cut originatingfrom biomass and more particularly for the reactions of hydrogenation,hydrodenitrogenation, hydrodearomatization, hydrodesulphurization,hydrodeoxygenation, hydrodemetallization or hydroconversion ofhydrocarbon-containing feedstocks.

In these uses, the catalyst according to the invention, which preferablyhas undergone a sulphurization step beforehand, has improved activitywith respect to the catalysts of the prior art. This catalyst may alsoadvantageously be used during pre-treatment of the feedstocks forcatalytic cracking or hydrocracking, or hydrodesulphurization ofresidues or deep hydrodesulphurization of diesels (ULSD, Ultra LowSulphur Diesel).

The feedstocks used in the hydrotreatment process are for examplegasolines, gasoils, vacuum gasoils, atmospheric residues, vacuumresidues, atmospheric distillates, vacuum distillates, heavy fuel oils,oils, waxes and paraffins, used oils, deasphalted residues or crudeoils, feedstocks obtained from thermal or catalytic conversionprocesses, lignocellulosic feedstocks or more generally feedstocksoriginating from biomass, used alone or in a mixture. The feedstocksthat are treated, and in particular those mentioned above, generallycontain heteroatoms such as sulphur, oxygen and nitrogen, and for theheavy feedstocks, most often they also contain metals.

The operating conditions used in the processes utilizing the reactionsof hydrotreatment of hydrocarbon-containing feedstocks described aboveare generally as follows: the temperature is advantageously comprisedbetween 180 and 450° C., and preferably between 250 and 440° C., thepressure is advantageously comprised between 0.5 and 30 MPa, andpreferably between 1 and 18 MPa, the hourly space velocity isadvantageously comprised between 0.1 and 20 h⁻¹ and preferably between0.2 and 5 h⁻¹, and the hydrogen/feedstock ratio expressed as volume ofhydrogen, measured under standard conditions of temperature andpressure, per volume of liquid feedstock is advantageously comprisedbetween 50 l/l and 5,000 l/l and preferably from 80 to 2,000 l/l.

According to a first method of use, said hydrotreatment processaccording to the invention is a process of hydrotreatment, and inparticular of hydrodesulphurization (HDS) of a gasoil cut, carried outin the presence of at least one catalyst according to the invention.Said hydrotreatment process according to the invention aims to removethe sulphur-containing compounds present in said gasoil cut so as toreach the current environmental standards, namely a permitted sulphurcontent of up to 10 ppm. It also makes it possible to lower the contentsof aromatics and nitrogen in the gasoil cut to be hydrotreated.

Said gasoil cut to be hydrotreated according to the process of theinvention contains 0.02 to 5.0% by weight of sulphur. It advantageouslyoriginates from direct distillation (or straight run gasoil), from acoking unit, from a visbreaking unit, from a steam cracking unit, from aunit for hydrotreatment and/or hydrocracking of heavier feedstocksand/or from a catalytic cracking unit (Fluid Catalytic Cracking). Saidgasoil cut preferably has at least 90% of compounds the boiling point ofwhich is comprised between 250° C. and 400° C. at atmospheric pressure.

The process for hydrotreatment of said gasoil cut according to theinvention is carried out under the following operating conditions: atemperature comprised between 200 and 400° C., preferably between 300and 380° C., a total pressure comprised between 2 MPa and 10 MPa andmore preferably between 3 MPa and 8 MPa with a ratio of volume ofhydrogen to volume of hydrocarbon-containing feedstock, expressed asvolume of hydrogen, measured under standard conditions of temperatureand pressure, per volume of liquid feedstock, comprised between 100 and600 litres per litre and more preferably between 200 and 400 litres perlitre and an hourly space velocity comprised between 1 and 10 h⁻¹,preferably between 2 and 8 h⁻¹. The HSV corresponds to the inversecontact time expressed in hours and is defined by the ratio of thevolume flow rate of liquid hydrocarbon-containing feedstock to thevolume of catalyst loaded in the reaction unit utilizing thehydrotreatment process according to the invention. The reaction unitcarrying out the process for the hydrotreatment of said gasoil cutaccording to the invention is preferably operated in a fixed bed, amoving bed or an ebullating bed, preferably in a fixed bed.

According to a second method of use, said hydrotreatment and/orhydrocracking process according to the invention is a process forhydrotreatment (in particular hydrodesulphurization,hydrodenitrogenation, hydrogenation of aromatics) and/or hydrocrackingof a vacuum distillate cut carried out in the presence of at least onecatalyst according to the invention. Said hydrotreatment and/orhydrocracking process, otherwise called process of hydrocrackingpre-treatment or hydrocracking according to the invention, aims,depending on the case, to remove the sulphur-containing,nitrogen-containing or aromatic compounds present in said distillate cutso as to carry out a pre-treatment prior to conversion in catalyticcracking or hydroconversion processes, or for hydrocracking thedistillate cut, which would optionally have been pre-treated beforehandif required.

Very varied feedstocks can be treated by the processes for thehydrotreatment and/or hydrocracking of vacuum distillates describedabove. Generally they contain at least 20% volume and often at least 80%volume of compounds boiling above 340° C. at atmospheric pressure. Thefeedstock may be for example vacuum distillates as well as feedstocksoriginating from units for extracting aromatics from lubricating oilbases or originating from solvent dewaxing of lubricating oil bases,and/or of deasphalted oils, or the feedstock may be a deasphalted oil orparaffins originating from the Fischer-Tropsch process or any mixture ofthe feedstocks mentioned above. In general, the feedstocks have a T5boiling point greater than 340° C. at atmospheric pressure, and betterstill greater than 370° C. at atmospheric pressure, i.e. 95% of thecompounds present in the feedstock have a boiling point greater than340° C., and better still greater than 370° C. The nitrogen content ofthe feedstocks treated in the processes according to the invention isusually greater than 200 ppm by weight, preferably comprised between 500and 10,000 ppm by weight. The sulphur content of the feedstocks treatedin the processes according to the invention is usually comprised between0.01 and 5.0% by weight. The feedstock may optionally contain metals(for example nickel and vanadium). The asphaltenes content is generallyless than 3,000 ppm by weight.

The hydrotreatment and/or hydrocracking catalyst is generally broughtinto contact, in the presence of hydrogen, with the feedstocks describedabove, at a temperature greater than 200° C., often comprised between250° C. and 480° C., advantageously comprised between 320° C. and 450°C., preferably between 330° C. and 435° C., at a pressure greater than 1MPa, often comprised between 2 and 25 MPa, preferably between 3 and 20MPa, the space velocity being comprised between 0.1 and 20.0 h⁻¹ andpreferably 0.1-6.0 h⁻¹, preferably 0.2-3.0 h⁻¹, and the quantity ofhydrogen introduced is such that the volume ratio litre ofhydrogen/litre of hydrocarbon, expressed as volume of hydrogen, measuredunder standard conditions of temperature and pressure, per volume ofliquid feedstock, is comprised between 80 and 5,000 l/l and most oftenbetween 100 and 2,000 l/l. These operating conditions used in theprocesses according to the invention generally make it possible to reachconversions per pass, in products having boiling points of less than340° C. at atmospheric pressure, and better still less than 370° C. atatmospheric pressure, greater than 15% and even more preferablycomprised between 20 and 95%.

The processes for the hydrotreatment and/or hydrocracking of vacuumdistillates utilizing the catalysts according to the invention cover theranges of pressure and of conversion ranging from mild hydrocracking tohigh-pressure hydrocracking. By mild hydrocracking is meanthydrocracking leading to moderate conversions, generally less than 40%,and operating at low pressure, generally between 2 MPa and 6 MPa.

The catalyst according to the invention may be used alone, in a singleor in several catalyst beds in fixed-bed mode, in one or more reactors,in a so-called one-step hydrocracking system, with or without liquidrecycling of the unconverted fraction, or in a so-called two-stephydrocracking system, optionally in combination with a hydrorefiningcatalyst located upstream of the catalyst of the present invention.

According to a third method of use, said hydrotreatment and/orhydrocracking process according to the invention is advantageously usedas pre-treatment in a fluidized-bed catalytic cracking process (or FCCprocess for Fluid Catalytic Cracking). The operating conditions of thepre-treatment in terms of temperature range, pressure range, hydrogenrecycle ratio, and hourly space velocity are generally identical tothose described above for the processes for the hydrotreatment and/orhydrocracking of vacuum distillates. The FCC process may be carried outconventionally as known to a person skilled in the art under suitablecracking conditions in order to produce hydrocarbon-containing productsof lower molecular weight. A brief description of catalytic crackingwill be found for example in ULLMANS ENCYCLOPEDIA OF INDUSTRIALCHEMISTRY VOLUME A 18, 1991, pages 61 to 64.

According to a fourth method of use, said hydrotreatment and/orhydrocracking process according to the invention is a process for thehydrotreatment (in particular hydrodesulphurization) of a gasoline cutin the presence of at least one catalyst according to the invention.

In contrast to other hydrotreatment processes, the hydrotreatment (inparticular hydrodesulphurization) of gasolines must make it possible tomeet two contradictory requirements: to ensure deephydrodesulphurization of the gasolines and to limit the hydrogenation ofthe unsaturated compounds present, in order to limit the loss of octanenumber.

The feedstock is generally a hydrocarbon cut having a distillation rangecomprised between 30 and 260° C. Preferably, this hydrocarbon cut is acut of the gasoline type. Very preferably, the gasoline cut is anolefinic gasoline cut originating for example from a catalytic crackingunit (Fluid Catalytic Cracking).

The hydrotreatment process consists of bringing the hydrocarbon cut intocontact with the catalyst according to the invention and hydrogen underthe following conditions: at a temperature comprised between 200 and400° C., preferably comprised between 230 and 330° C., at a totalpressure comprised between 1 and 3 MPa, preferably comprised between 1.5and 2.5 MPa, at an hourly space velocity (HSV), defined as the volumeflow rate of feedstock with respect to the volume of catalyst, comprisedbetween 1 and 10 h⁻¹, preferably comprised between 2 and 6 h⁻¹ and at ahydrogen/gasoline feedstock volume ratio comprised between 100 and 600Nl/l, preferably comprised between 200 and 400 Nl/l.

The process for the hydrotreatment of the gasolines may be carried outin one or more reactors in series of the fixed bed type or of theebullating bed type. If the process is carried out by means of at leasttwo reactors in series, it is possible to provide a device for removingH₂S from the effluent originating from the first hydrodesulphurizationreactor before treating said effluent in the secondhydrodesulphurization reactor.

The examples given below demonstrate the significantly increasedactivity on the catalysts prepared by the process according to theinvention with respect to the catalysts of the prior art and explain theinvention but without however limiting its scope.

EXAMPLES Example 1: Preparation of the CoMoP Catalysts on Aluminawithout Organic Compound C1 and C2 (not According to the Invention)

Cobalt, molybdenum and phosphorus are added to an alumina support havinga BET surface area of 230 m²/g, a pore volume obtained by mercuryporosimetry of 0.78 ml/g and an average diameter of the pores of 11.5 nmdefined as the median diameter by volume by mercury porosimetry andwhich is in the form of “extrudate”. The impregnating solution isprepared by dissolving molybdenum oxide (24.34 g) and cobalt hydroxide(5.34 g) at 90° C. in 7.47 g of an 85% solution of phosphoric acid inwater. After dry impregnation, the extrudates are left to mature in awater-saturated atmosphere for 12 h at ambient temperature, then theyare dried at 90° C. for 16 hours. The dried catalyst precursor thusobtained is denoted C1. Calcining the catalyst precursor C1 at 450° C.for 2 hours results in the calcined catalyst C2. The final compositionof catalysts C1 and C2 expressed in the form of oxides and referenced tothe mass of dry catalyst is then as follows: MoO₃=22.5±0.2% by weight,CoO=4.1±0.1% by weight and P₂O₅=4.0±0.1% by weight.

Example 2: Preparation of the CoMoP Catalysts on Alumina C3 and C4 (notAccording to the Invention), and C5 (According to the Invention) byCo-Impregnation

Cobalt, molybdenum and phosphorus are added to the alumina supportdescribed above in Example 1, which is in the form of “extrudate”. Theimpregnating solution is prepared by dissolving molybdenum oxide (28.13g) and cobalt hydroxide (6.62 g) at 90° C. in 7.88 g of an 85% solutionof phosphoric acid in water. After homogenizing the above mixture, 37.79g of citric acid was added before adjusting the solution volume to thepore volume of the support by adding water. The (citric acid)/Mo molarratio is equal to 1 mol/mol and the (citric acid)/Co molar ratio isequal to 2.8 mol/mol. After dry impregnation, the extrudates are left tomature in a water-saturated atmosphere for 12 h at ambient temperature,and then they are dried at 120° C. for 16 hours. The dried catalystprecursor thus obtained is denoted C3. The final composition of catalystC3, expressed in the form of oxides and referenced to the mass of drycatalyst, is then as follows: MoO₃=22.7±0.2% by weight, CoO=4.2±0.1% byweight and P₂O₅=3.8±0.1% by weight.

The catalyst C4 is prepared in a similar way to the catalyst C3, butafter homogenizing the metallic solution containing cobalt, molybdenumand phosphorus, triethylene glycol (TEG) is added, once again in aproportion of 1 mole per mole of molybdenum or 2.8 moles per mole ofcobalt. The catalyst C4 was left to mature in a water-saturatedatmosphere for 12 hours at ambient temperature, and then dried at 120°C. for 16 hours. The final composition of the catalyst C4, expressed inthe form of oxides and referenced to the mass of dry catalyst, is thenas follows: MoO₃=22.6±0.2% by weight, CoO=4.1±0.1% by weight andP₂O₅=3.9±0.1% by weight.

The catalyst C5 according to the invention is prepared as follows.Cobalt, molybdenum and phosphorus are added to the alumina supportdescribed in Example 1, which is in the form of “extrudate”. Animpregnating solution was prepared by dissolving molybdenum oxide (78.75g) and cobalt hydroxide (18.54 g) at 90° C. in 22.08 g of an 85%solution of phosphoric acid in water. After homogenizing the abovemixture, γ-ketovaleric acid was added to the solution, in equimolarproportions with respect to the molybdenum, i.e. 2.8 moles per mole ofcobalt before adjusting the solution volume to the pore volume of thesupport by adding water. After dry impregnation, the extrudates of thecatalyst were left to mature in a water-saturated atmosphere for 12hours at ambient temperature, and then dried at 120° C. for 16 hours.The final composition of the catalyst C5 expressed in the form of oxidesand referenced to the mass of dry catalyst is then as follows:MoO₃=22.4±0.2% by weight, CoO=4.0±0.1% by weight and P₂O₅=4.0±0.1% byweight.

Example 3: Preparation of the CoMoP Catalyst on Alumina C6 (According tothe Invention) by Pre-Impregnation

24.7 g of γ-ketovaleric acid diluted in water, so as to obtain asolution with a total volume equal to the pore volume of the support, isadded to the alumina support described above in Example 1, which is inthe form of “extrudate”. The solution thus formed is thendry-impregnated on the support before observing a maturation time of 3hours in a water-saturated atmosphere at ambient temperature, followedby drying at 120° C. for 2 hours. The modified support is thenimpregnated with a fresh impregnating solution prepared by hotdissolution of molybdenum oxide (27.00 g) and cobalt hydroxide (6.36 g)in 7.57 g of an 85% solution of phosphoric acid in water, taking care toadjust the volume of this last-mentioned solution to the pore volume ofthe previous modified support, by adding water. After dry impregnation,the extrudates were left to mature in a water-saturated atmosphere for 3h at ambient temperature, and then dried at 120° C. for 16 hours,resulting in the catalyst C6. The final composition of the catalyst C6expressed in the form of oxides and referenced to the mass of drycatalyst is then as follows: MoO₃=22.5±0.2% by weight, CoO=4.1±0.1% byweight and P₂O₅=4.0±0.1% by weight. The quantities used are such thatthe quantity of γ-ketovaleric acid is one mole per mole of molybdenumand 2.8 moles per mole of cobalt.

Example 4: Preparation of the CoMoP Catalysts on Alumina C7 (notAccording to the Invention) and C8 (According to the Invention) byCo-Impregnation (Low Organic Compound/Mo Ratio)

Cobalt, molybdenum and phosphorus are added to the alumina supportdescribed above in Example 1, which is in the form of “extrudate”, asfor the preparation of the catalyst C3. However, during preparation ofthe impregnating solution, the citric acid/molybdenum molar ratio is inthis case equal to 0.25 mol/mol, or 0.70 mole of citric acid per mole ofcobalt. After dry impregnation, the extrudates are left to mature in awater-saturated atmosphere for 12 hours at ambient temperature, and thenthey are dried at 120° C. for 16 hours. The dried catalyst precursorthus obtained is denoted C7. The final composition of the catalyst C7,expressed in the form of oxides and referenced to the mass of drycatalyst, is then as follows: MoO₃=22.5±0.2% by weight, CoO=4.0±0.1% byweight and P₂O₅=3.9±0.1% by weight.

Cobalt, molybdenum and phosphorus are added to the alumina supportdescribed above in Example 1, which is in the form of “extrudate”, asfor the preparation of the catalyst C5. However, during preparation ofthe impregnating solution, the molar ratio of γ-ketovaleric acid tomolybdenum was fixed at 0.25 mol/mol, i.e. 0.70 mole of γ-ketovalericacid per mole of cobalt. After dry impregnation, the extrudates wereleft to mature in a water-saturated atmosphere for 12 hours at ambienttemperature, and then dried at 120° C. for 16 hours. The dried catalystprecursor thus obtained is denoted C8. The final composition of thecatalyst C8 expressed in the form of oxides and referenced to the massof dry catalyst is then as follows: MoO₃=22.3±0.2% by weight,CoO=4.1±0.1% by weight and P₂O₅=4.3±0.1% by weight.

Example 5: Evaluation of the Catalysts C1, C2, C3, C4 and C7 (notAccording to the Invention) and C5, C6 and C8 (According to theInvention) in the HDS of Gasoil

The catalysts C1, C2, C3, C4 and C7 (not according to the invention) andC5, C6, C8 (according to the invention) were tested in the HDS ofgasoil.

Characteristics of the gasoil feedstock used:

Density at 15° C.: 0.8522 g/cm³ Sulphur: 1.44% by weight SimulatedDistillation: IBP: 155° C. 10%: 247° C. 50%: 315° C. 90%: 392° C. FBP:444° C.

The test is carried out in an isothermal pilot reactor with atransversed fixed bed, with the fluids circulating from bottom to top.After sulphurization in situ at 350° C. in the unit under pressure bymeans of the gasoil for the test, to which 2% by weight of dimethyldisulphide is added, the hydrodesulphurization test was carried outunder the following operating conditions: total pressure of 7 MPa,catalyst volume of 30 cm³, temperature from 330 to 360° C., hydrogenflow rate of 24 I/h and feedstock flow rate of 60 cm³/h.

The catalytic performances of the catalysts tested are shown in Table 1.They are is expressed in degrees Celsius based on a comparative catalystselected as reference (C2): they correspond to the temperaturedifference to be applied to achieve 50 ppm of sulphur in the effluent. Anegative value indicates that the target sulphur content is reached fora lower temperature and that there is therefore a gain of activity. Apositive value means that the target sulphur content is reached for ahigher temperature and that there is therefore a loss of activity. Theresults obtained are presented in Table 1.

Table 1 clearly shows the gain in catalytic effect provided byγ-ketovaleric acid. In fact, the catalysts C5 and C6 (according to theinvention) have activities greater than those obtained for all the othercatalysts evaluated for the same molar proportions of organic compound(1 mol/mol_(Mo)).

The gain is also maximized, for the same quantity of additive; thecatalysts C5 is more active than the catalysts C3 and C4 respectivelyobtained with citric acid or TEG which are 4.7° C. and 2.5° C. lessactive.

The activity of the catalyst C6 is still far higher than that of thebase catalyst C2 or of a dried catalyst C1 without γ-ketovaleric acid.

The advantage of the catalyst according to the invention is stillsignificant at a lower proportion of organic compound, as shown by thecatalyst C8, which thus has an intrinsic effectiveness of γ-ketovalericacid greater than that of the other compounds, for which it is necessaryto introduce a higher proportion of compound in order to observe asignificant catalytic effect.

TABLE 1 Relative activity at iso-volume of the catalysts C1, C2, C3, C4and C7 (not according to the invention) and C5, C6, C8 (according to theinvention) with respect to the catalyst C2 (not according to theinvention), in the hydrodesulphurization of gasoil Catalyst Method ofintroducing (comparative the organic compound or according Organiccompound used (post-/co-/pre- Heat to the invention) and molar ratio/Moimpregnation) treatment HDS activity C1 (comp) none N/A Dried Base +1.1° C. 120° C. C2 (comp) none N/A Calcined Base C3 (comp) Citric acid -1.0 CO Dried Base − 3.1° C. 120° C. C4 (comp) TEG - 1.0 CO Dried Base −5.3° C. 120° C. C5 (inv) γ-ketovaleric acid - 1.0 CO Dried Base − 7.8°C. 120° C. C6 (inv) γ-ketovaleric acid - 1.0 PRE Dried Base − 6.5° C.120° C. C7 (comp) Citric acid - 0.25 CO Dried Base − 2.2° C. 120° C. C8(inv) γ-ketovaleric acid - CO Dried Base − 4.2° C. 0.25 120° C.

1. Catalyst comprising a support based on alumina or silica orsilica-alumina, at least one element of group VIII, at least one elementof group VIB, and γ-ketovaleric acid.
 2. Catalyst according to claim 1,in which the content of the element of group VIB is comprised between 5and 40% by weight expressed as oxide of the metal of group VIB withrespect to the total weight of the catalyst and the content of theelement of group VIII is comprised between 1 and 10% by weight expressedas oxide of the metal of group VIII with respect to the total weight ofthe catalyst.
 3. Catalyst according to claim 1, in which the molar ratioof the element of group VIII to the element of group VIB in the catalystis between 0.1 and 0.8.
 4. Catalyst according to claim 1, whichadditionally contains phosphorus, the phosphorus content being comprisedbetween 0.1 and 20% by weight expressed as P₂O₅ with respect to thetotal weight of the catalyst and the ratio of phosphorus to the elementof group VIB in the catalyst is greater than or equal to 0.05. 5.Catalyst according to claim 1, in which the content of γ-ketovalericacid is comprised between 1 and 35% by weight with respect to the totalweight of the catalyst.
 6. Catalyst according to claim 1, whichadditionally contains an organic compound other than γ-ketovaleric acidcontaining oxygen and/or nitrogen and/or sulphur.
 7. Catalyst accordingto claim 6, in which the organic compound is selected from a compoundcomprising one or more chemical functions selected from a carboxyl,alcohol, thiol, thioether, sulphone, sulphoxide, ether, aldehyde,ketone, ester, carbonate, amine, nitrile, imide, oxime, urea and amidefunction.
 8. Catalyst according to claim 7, in which the organiccompound is selected from triethylene glycol, diethylene glycol,ethylenediaminetetraacetic acid, maleic acid, citric acid,dimethylformamide, bicine, or tricine.
 9. Catalyst according to claim 1,in which the support contains from 0.1 to 50% by weight of zeolite. 10.Catalyst according to claim 1, characterized in that it is at leastpartially sulphurized.
 11. Process for the preparation of a catalystaccording to claim 1 comprising the following steps: a) bringing atleast one component of an element of group VIB, at least one componentof an element of group VIII, γ-ketovaleric acid and optionallyphosphorus into contact with a support based on alumina or silica orsilica-alumina, or bringing a regenerated catalyst containing a supportbased on alumina or silica or silica-alumina, at least one component ofan element of group VIB, at least one component of an element of groupVIII and optionally phosphorus into contact with γ-ketovaleric acid, soas to obtain a catalyst precursor, b) drying said catalyst precursororiginating from step a) at a temperature of less than 200° C., withoutcalcining it subsequently.
 12. Process according to claim 11, in whichstep a) is the following step: a′) impregnating a support based onalumina or silica or silica-alumina with at least one solutioncontaining at least one element of group VIB, at least one element ofgroup VIII, γ-ketovaleric acid and optionally phosphorus so as to obtaina catalyst precursor.
 13. Process according to claim 11, in which stepa) comprises the following steps: a1) impregnating a support based onalumina or silica or silica-alumina with at least one solutioncontaining at least one element of group VIB, at least one element ofgroup VIII and optionally phosphorus in order to obtain an impregnatedsupport, a2) drying the impregnated support obtained in step a1) at atemperature of less than 200° C. in order to obtain a dried impregnatedsupport, and optionally calcining the dried impregnated support in orderto obtain a calcined impregnated support, a3) impregnating the dried andoptionally calcined impregnated support obtained in step a2) with animpregnating solution comprising at least γ-ketovaleric acid so as toobtain a catalyst precursor, a4) optionally, leaving the catalystprecursor obtained in step a3) to mature.
 14. Process according to claim11, in which step a) comprises the following steps: a1′) preparing asupport comprising at least γ-ketovaleric acid and optionally at leastone part of phosphorus, a2′) impregnating the support obtained in stepa1′) with an impregnating solution comprising at least one element ofgroup VIB, at least one element of group VIII and optionally phosphorusso as to obtain a catalyst precursor, a3′) optionally, leaving thecatalyst precursor obtained in step a2′) to mature.
 15. Processaccording to claim 11, in which step a) comprises the following steps:a1″) by co-impregnation, bringing a solution containing at least oneelement of group VIB, at least one element of group VIII, at least oneorganic compound containing oxygen and/or nitrogen and/or sulphur, andoptionally phosphorus into contact with a support based on alumina orsilica or silica-alumina so as to obtain an impregnated support, a2″)drying the impregnated support originating from step a1″) at atemperature of less than 200° C., without calcining it subsequently, inorder to obtain a dried impregnated support, a3″) bringing the driedimpregnated support originating from step a2″) into contact with asolution of an organic compound containing oxygen and/or nitrogen and/orsulphur, identical to or different from that used in step a1″), so as toobtain a catalyst precursor, a4″) optionally, leaving the catalystprecursor obtained in step a3″) to mature, and at least one of theorganic compounds in step a1″) or in step a3″) is γ-ketovaleric acid.16. Process according to claim 11, in which step a) comprises thefollowing steps: a1′″) impregnating a regenerated catalyst containing asupport based on alumina or silica or silica-alumina, at least onecomponent of an element of group VIB, at least one component of anelement of group VIII and optionally phosphorus with an impregnatingsolution comprising at least γ-ketovaleric acid so as to obtain acatalyst precursor, a2′″) optionally, leaving the catalyst precursorobtained in step a1′″) to mature.
 17. Process according to claim 11, inwhich the molar ratio of γ-ketovaleric acid to the element(s) of groupVIII is comprised between 0.1 and 5.0 mol/mol.
 18. A process for thehydrotreatment and/or hydrocracking of hydrocarbon-containing cuts,comprising subjecting said hydrocarbon-containing cut to hydrotreatmentor hydrocracking conditions in the presence of a catalyst according toclaim 1.